Severely sterically hindered secondary aminoether alcohols

ABSTRACT

A novel class of severely sterically hindered secondary aminoether alcohols of the general formula: ##STR1## are prepared wherein R 1  and R 2  are each selected from the group consisting of alkyl and hydroxylalkyl radicals R 3 , R 4 , R 5  and R 6  are each selected from the group consisting of hydrogen, alkyl and hydroxyalkyl radicals, with the proviso that at least one of R 4  or R 5  bonded to the carbon atom directly bonded to the nitrogen atom is an alkyl or hydroxyalkyl radical when R 3  is hydrogen, x and y are each positive integers ranging from 2-4 and z is a positive integer ranging from 1-4. The compounds are useful in the selective removal of H 2  S from mixtures containing H 2  S and CO 2 .

This is a division of application Ser. No. 453,452, filed Dec. 27, 1982, now U.S. Pat. No. 4,471,138 and a continuation-in-part application of copending U.S. application Ser. Nos. 339,892 and 418,751 filed Jan. 18, 1982, abandoned and Sept. 16, 1982, respectively.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to a class of severely sterically hindered secondary aminoether alcohols and their preparation. These compounds are useful, for example, in the removal of hydrogen sulfide from normally gaseous streams containing hydrogen sulfide, including selective removal from such streams which also contain carbon dioxide.

2. Description of Related Patents

It is well-known in the art to treat gases and liquids, such as mixtures containing acidic gases including CO₂, H₂ S, CS₂, HCN, COS and oxygen and sulfur derivatives of C₁ to C₄ hydrocarbons with amine solutions to remove these acidic gases. The amine usually contacts the acidic gases and the liquids as an aqueous solution containing the amine in an absorber tower with the aqueous amine solution contacting the acidic fluid countercurrently.

The treatment of acid gas mixtures containing, inter alia, CO₂ and H₂ S, with amine solutions typically results in the simultaneous removal of substantial amounts of both the CO₂ and H₂ S. For example, in one such process generally referred to as the "aqueous amine process," relatively concentrated amine solutions are employed. A recent improvement on this process involves the use of sterically hindered amines as described in U.S. Pat. No. 4,112,052, to obtain nearly complete removal of acid gases such as CO₂ and H₂ S. This type of process may be used where the partial pressures of the CO₂ and related gases are low. Another process often used for specialized applications where the partial pressure of CO₂ is extremely high and/or where many acid gases are present, e.g., H₂ S, COS, CH₃ SH and CS₂ involves the use of an amine in combination with a physical absorbent, generally referred to as the "nonaqueous solvent process." An improvement on this process involves the use of sterically hindered amines and organic solvents as the physical absorbent such as described in U.S. Pat. No. 4,112,051.

It is often desirable, however, to treat acid gas mixtures containing both CO₂ and H₂ S so as to remove the H₂ S selectively from the mixture, thereby minimizing removal of the CO₂. Selective removal of H₂ S results in a relatively high H₂ S/CO₂ ratio in the separated acid gas which simplifies the conversion of H₂ S to elemental sulfur using the Claus process.

The typical reactions of aqueous secondary and tertiary amines with CO₂ and H₂ S can be represented as follows:

    H.sub.2 S+R.sub.3 N⃡R.sub.3 NH.sup.+ +SH.sup.- ( 1)

    H.sub.2 S+R.sub.2 NH⃡R.sub.2 NH.sub.2.sup.+ +SH.sup.-( 2)

    CO.sub.2 +R.sub.3 N+H.sub.2 O⃡R.sub.3 NH.sup.+ +HCO.sub.3 -(3)

    CO.sub.2 +2R.sub.2 NH⃡R.sub.2 NH.sub.2.sup.+ +R.sub.2 NCOO.sup.-( 4)

wherein R is an organic radical which may be the same or different and may be substituted with a hydroxyl group. The above reactions are reversible, and the partial pressures of both CO₂ and H₂ S are thus important in determining the degree to which the above reactions occur.

While selective H₂ S removal is applicable to a number of gas treating operations including treatment of hydrocarbon gases from shale pyrolysis, refinery gas and natural gas having a low H₂ S/CO₂ ratio, it is particularly desirable in the treatment of gases wherein the partial pressure of H₂ S is relatively low compared to that of CO₂ because the capacity of an amine to absorb H₂ S from the latter type gases is very low. Examples of gases with relatively low partial pressures of H₂ S include synthetic gases made by coal gasification, sulfur plant tail gas and low Joule fuel gases encountered in refineries where heavy residual oil is being thermally converted to lower molecular weight liquids and gases.

Although it is known that solutions of primary and secondary amines such as monoethanolamine (MEA), diethanolamine (DEA), dipropanolamine (DPA), and hydroxyethoxyethylamine (DGA) absorb both H₂ S and CO₂ gas, they have not proven especially satisfactory for preferential absorption of H₂ S to the exclusion of CO₂ because the amines undergo a facile reaction with CO₂ to form carbamates.

Diisopropanolamine (DIPA) is relatively unique among secondary aminoalcohols in that it has been used industrially, alone or with a physical solvent such as sulfolane, for selective removal of H₂ S from gases containing H₂ S and CO₂, but contact times must be kept relatively short to take advantage of the faster reaction of H₂ S with the amine compared to the rate of CO₂ reaction as shown in Equations 2 and 4 hereinabove.

In 1950, Frazier and Kohl, Ind. and Eng. Chem., 42, 2288 (1950) showed that the tertiary amine, methyldiethanolamine (MDEA), has a high degree of selectivity toward H₂ S absorption over CO₂. This greater selectivity was attributed to the relatively slow chemical reaction of CO₂ with tertiary amines as compared to the rapid chemical reaction of H₂ S. The commercial usefulness of MDEA, however, is limited because of its restricted capacity for H₂ S loading and its limited ability to reduce the H₂ S content to the level at low pressures which is necessary for treating, for example, synthetic gases made by coal gasification.

Recently, U.K. Patent Publication 2,017,524A to Shell disclosed that aqueous solutions of dialkylmonoalkanolamines, and particularly diethylmonoethanolamine (DEAE), have higher selectivity and capacity for H₂ S removal at higher loading levels than MDEA solutions. Nevertheless, even DEAE is not very effective for the low H₂ S loading frequently encountered in the industry. Also, DEAE has a boiling point of 161° C., and as such, it is characterized as being a low-boiling, relatively highly volatile amino alcohol. Such high volatilities under most gas scrubbing conditions result in large material losses with consequent losses in economic advantages.

SUMMARY OF THE INVENTION

It has now been discovered that absorbent solutions of a certain class of amino compounds defined as severely sterically hindered acyclic secondary aminoether alcohols have a high selectivity for H₂ S compared to CO₂. These amino compounds surprisingly maintain their high selectivity at high H₂ S and CO₂ loadings.

This specific class of severely sterically hindered secondary aminoether alcohols are defined by the general formula: ##STR2## wherein R₁ and R₂ are each independently selected from the group consisting of alkyl or hydroxyalkyl radicals having 1-4 carbon atoms, R₃, R₄, R₅ and R₆ are each independently selected from the group consisting of hydrogen, alkyl or hydroxyalkyl radicals having 1-4 carbon atoms, with the proviso that at least one of R₄ or R₅ bonded to the carbon atom which is directly bonded to the nitrogen atom is an alkyl or hydroxyalkyl radical having 1-4 carbon atoms when R₃ is hydrogen, x and y are each positive integers ranging from 2-4 and z is a positive integer ranging from 1-4.

By the term "severely sterically hindered" it is meant that the nitrogen atom is attached to one or more bulky carbon groupings. Typically, these severely sterically hindered secondary aminoether alcohols will have a degree of steric hindrance such that the cumulative -E_(s) value (Taft's steric hindrance constant) is greater than about 1.75 as calculated from the values given for primary amines in Table V from the article by D. F. DeTar, Journal of Organic Chemistry, 45, 5174 (1980), the entire disclosure of which is incorporated herein by reference.

Another means for determining whether a secondary amino compound is "severely sterically hindered" is by measuring its ¹⁵ N nuclear magnetic resonance (NMR) chemical shift. By such measurements it has been found that the "ordinary sterically hindered" secondary amino compounds have a ¹⁵ N NMR chemical shift greater than about δ+40 ppm, when a 90% by wt. amine solution in 10% by wt. D₂ O at 35° C. is measured by a spectrometer using liquid (neat) ammonia at 25° C. as a zero reference value. For example, the severely sterically hindered amino compounds, 2-(2-tertiarybutylamino)propoxyethanol, 3-(tertiarybutylamino)-1-propanol, 2-(2-isopropylamino)propoxyethanol and tertiarybutylaminoethoxyethanol had measured ¹⁵ N NMR chemical shift values of δ+74.3, δ+65.9, δ+65.7 and δ+60.5 ppm, respectively, whereas the ordinary sterically hindered amine, secondarybutylaminoethoxyethanol, and the non-sterically hindered amine, n-butylaminoethoxyethanol, had measured ¹⁵ N NMR chemical shift values of δ+48.9 and δ+35.8 ppm, respectively. When the cumulative ⁻ E_(s) values (Taft's steric hindrance constant of these amines) is plotted against the ¹⁵ N NMR chemical shift values of the amino compounds mentioned above, a straight line is observed. As evident in the data shown herein, those amino compounds analyzed having ¹⁵ N NMR chemical shift values greater than δ+50 ppm under the test conditions described above had a higher H₂ S selectivity than those amino compounds having a ¹⁵ N NMR chemical shift values less than δ+50 ppm. The tertiary amino compound used for comparison herein, methyldiethanolamine, had a measured ¹⁵ N NMR chemical shift value of δ+27.4 ppm.

Another embodiment of the invention relates to the non-catalytic preparation of these novel compounds by a high temperature reaction of a secondary or tertiary alkyl primary amine with an ether alcohol containing a carbonyl functionality in the process of a source of hydrogen or with a haloalkoxyalkanol.

The class of severely sterically hindered secondary aminoether alcohols herein may be used in a process for the absorption of H₂ S, preferably the selective absorption of H₂ S from a normally gaseous mixture containing H₂ S and CO₂ comprising:

(a) contacting said normally gaseous mixture with an absorbent solution comprising severely sterically hindered acyclic secondary aminoether alcohols under conditions such that H₂ S is selectively absorbed from said mixture;

(b) regenerating, at least partially, said absorbent solution containing H₂ S; and

(c) recycling the regenerated solution for the selective absorption of H₂ S by contacting as in step (a).

Preferably, the regeneration step is carried out by heating and stripping and more preferably heating and stripping with steam.

The term "normally gaseous" herein refers to ambient conditions of temperature and pressure.

The amino absorbent is preferably one or more compounds selected from the group consisting of tertiary butylaminoethoxyethanol, 2-(2-tertiarybutylamino)propoxyethanol and 2-(2-isopropylamino)propoxyethanol. One of the preferred amino compounds is tertiarybutylaminoethoxyethanol (TBEE).

The amino compounds herein are further characterized by their low volatility and high solubility in water at selective H₂ S removal conditions, and most of the compounds are also generally soluble in polar organic solvent systems which may or may not contain water. The term "absorbent solution" as used herein includes but is not limited to solutions wherein the amino compound is dissolved in a solvent selected from water or a physical absorbent or mixtures thereof. Solvents which are physical absorbents (as opposed to the amino compounds which are chemical absorbents) are described, for example, in U.S. Pat. No. 4,112,051, the entire disclosure of which is incorporated herein by reference, and include, e.g., aliphatic acid amides, N-alkylated pyrrolidones, sulfones, sulfoxides, glycols and the mono- and diethers thereof. The preferred physical absorbents herein are sulfones, and most particularly, sulfolane.

The absorbent solution ordinarily has a concentration of amino compound of about 0.1 to 6 moles per liter of the total solution, and preferably 1 to 4 moles per liter, depending primarily on the specific amino compound employed and the solvent system utilized. If the solvent system is a mixture of water and a physical absorbent, the typical effective amount of the physical absorbent employed may vary from 0.1 to 5 moles per liter of total solution, and preferably from 0.5 to 3 moles per liter, depending mainly on the type of amino compound being utilized. The dependence of the concentration of amino compound on the particular compound employed is significant because increasing the concentration of amino compound may reduce the basicity of the absorbent solution, thereby adversely affecting its selectivity for H₂ S removal, particularly if the amino compound has a specific aqueous solubility limit which will determine maximum concentration levels within the range given above. It is important, therefore, that the proper concentration level appropriate for each particular amino compound be maintained to insure satisfactory results.

The solution of this invention may include a variety of additives typically employed in selective gas removal processes, e.g., antifoaming agents, antioxidants, corrosion inhibitors, and the like. The amount of these additives will typically be in the range that they are effective, i.e., an effective amount.

Also, the amino compounds described herein may be admixed with other amino compounds as a blend preferably with methyldiethanolamine. The mole ratio of the respective amino compounds may vary widely, for example, from 1 to 99 percent of the amino compounds described herein.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a diagrammatic flow sheet illustrating an absorption-regeneration unit for selective removal of H₂ S from gaseous streams containing H₂ S and CO₂.

FIG. 2 is a diagrammatic flow sheet illustrating an experimental sparged absorber unit for use in rapid determination of the selectivity of the amino compound for selective removal of H₂ S from gaseous streams containing H₂ S and CO₂.

FIG. 3 graphically illustrates the selectivity for H₂ S plotted against the H₂ S and CO₂ loading for tertiarybutylaminoethoxyethanol (TBEE) as compared to tertiarybutylaminoethanol (TBE) and methyldiethanolamine (MDEA).

FIG. 4 graphically illustrates the selectivity for H₂ S plotted against the H₂ S and CO₂ loading for tertiarybutylaminoethoxyethanol (TBEE) as compared to methyldiethanolamine (MDEA), secondarybutylaminoethoxyethanol (SBEE) and isopropylaminoethoxyethanol (IPEE).

FIG. 5 graphically illustrates the H₂ S leak rate plotted against H₂ S loading in moles/mole amine for tertiarybutylaminoethoxyethanol (TBEE) compared against methyldiethanolamine (MDEA).

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The compounds of the invention are preferably characterized by the following general formula: ##STR3## where: R₁ =R₂ =R₃ =CH₃ ; R₄ =R₅ =R₆ =H;

R₁ =R₂ =R₃ =CH₃ ; R₄ =H or CH₃ ; R₅ =R₆ =H;

R₁ =R₂ =R₃ =R₆ =CH₃ ; R₄ =R₅ =H;

R₁ =R₂ =R₃ =CH₃ CH₂ ; R₄ =R₅ =R₆ =H; or

R₁ ≠R₂ ≠R₃ =H; CH₃, CH₃ CH₂, R₄ ≠R₅ ≠R₆ =H or CH₃,

and where x=2-3.

The preferred compounds defined by the general formulae above include: ##STR4##

As another embodiment of the invention, these novel secondary aminoether alcohols are prepared by a process comprising reacting, at elevated temperatures, and preferably in the presence of a solvent, a secondary or tertiary alkyl primary amine with an ether alcohol containing a carbonyl functionality in the presence of a source of hydrogen, or with a haloalkoxyalkanol.

Typical secondary or tertiary alkyl primary amines useful in the process of the invention include isopropylamine, tertiarybutylamine, 1-methyl-1-ethylpropylamine, and tertiaryamylamine. Typical haloalkoxyalkanols include 2-chloroethoxyethanol and the like. Typical ether alcohols containing a carbonyl functionality (such as a ketone or aldehyde group include 6-hydroxy-3-oxa-2-hexanone. Typical solvents include lower alkanols, ether alkanols and acyclic and cyclic ethers and the secondary alkylamine reagent. Examples of typical solvents include water, methanol, ethanol, propanol, ethylene glycol monomethyl ether, tetrahydrofuran, isopropylamine, tertiarybutylamine, tertiaryamylamine and the like. Preferably, the solvent is a polar compound. The preferred solvents include water, methanol, ethanol and ethylene glycol monomethylether.

The elevated temperatures which may be employed herein for the reaction will depend on the particular type of reaction being carried out and on the particular amine employed and the pressures utilized. For the non-catalytic process wherein the amine is reacted with a haloalkoxyalkanol, the reaction temperatures employed are preferably at least 80° C. and more preferably at least 100° C. at atmospheric pressure. When elevated pressures are employed, e.g., autogenous pressure in an autoclave, this reaction is preferably carried out at temperatures of at least about 110° C. and preferably less than about 250° C., and more preferably from 125° C. to about 200° C. Suitable autogenous pessures range from 50 psig to about 1000 psig, more preferably 150 to about 400 psig. Such autogenous pressure conditions are particularly preferred in the synthesis of tertiarybutylaminoethoxyethanol.

For the process wherein the amine is reacted with an ether alcohol containing a carbonyl functionality in the presence of a source of hydrogen, the temperatures employed are preferably at least 80° C., more preferably 90° to 120° C. The latter reaction process may be carried out by a catalytic reductive amination in the presence of hydrogen gas, preferably at a pressure of 1000 to 1400 psig. Alternatively, the latter reaction process may be carried out by a non-catalytic reductive amination wherein the hydrogen source is a metal hydride.

In all types of reactions, the reaction mixture preferably contains a molar excess of the amine, preferably at least a 2:1 molar excess.

The amino ether alcohol compounds used in the absorbent process described above have a pK_(a) value at 20° C. greater than 8.6, preferably greater than about 9.5 and more preferably the pK_(a) value of the amino compound will range between about 9.5 and about 10.6. If the pK_(a) is less than 8.6 the reaction with H₂ S is decreased, whereas if the pK_(a) of the amino ether alcohol compound is much greater than about 10.6, an excessive amount of steam is required to regenerate the solution. Also, to insure operational efficiency with minimal losses of the amino compound, the amino compound should have a relatively low volatility. For example, the boiling point of the amine (at 760 mm) is typically greater than about 180° C., preferably greater than 200° C., and more preferably greater than 225° C.

Three characteristics which are of ultimate importance in determining the effectiveness of the amino compounds herein for H₂ S removal are "selectivity", "loading" and "capacity". The term "selectivity" as used throughout the specification is defined as the following mole ratio fraction: ##EQU1## The higher this fraction, the greater the selectivity of the absorbent solution for the H₂ S in the gas mixture.

By the term "loading" is meant the concentration of the H₂ S and CO₂ gases physically dissolved and chemically combined in the absorbent solution as expressed in moles of gas per moles of the amine. The best amino compounds are those which exhibit good selectivity up to a relatively high loading level. The amino compounds used in the practice of the present invention typically have a "selectivity" of not substantially less than 10 at a "loading" of 0.1 moles, preferably, a "selectivity" of not substantially less than 10 at a loding of 0.2 or more moles of H₂ S and CO₂ per mole of the amino compound.

"Capacity" is defined as the moles of H₂ S loaded in the absorbent solution at the end of the absorption step minus the moles of H₂ S loaded in the absorbent solution at the end of the desorption step. High capacity enables one to reduce the amount of amine solution to be circulated and use less heat or steam during regeneration.

The acid gas mixture herein necessarily includes H₂ S, and may optionally include other gases such as CO₂, N₂, CH₄, H₂, CO, H₂ O, COS, HCN, CO₂, H₄, NH₃, and the like. Often such gas mixtures are found in combustion gases, refinery gases, town gas, natural gas, syn gas, water gas, propane, propylene, heavy hydrocarbon gases, etc. The absorbent solution herein is particularly effective when the gaseous mixture is a gas, obtained, for example, from shale oil retort gas, coal or gasification of heavy oil with air/steam or oxygen/steam thermal conversion of heavy residual oil to lower molecular weight liquids and gases, or in sulfur plant tail gas clean-up operations.

The absorption step of this invention generally involves contacting the normally gaseous stream with a absorbent solution in any suitable contacting vessel. In such processes, the normally gaseous mixture containing H₂ S and CO₂ from which the H₂ S is to be selectively removed may be brought into intimate contact with the absorbent solution using conventional means, such as a tower or vessel packed with, for example, rings or with sieve plates, or a bubble reactor.

In a typical mode of practicing the invention, the absorption step is conducted by feeding the normally gaseous mixture into the lower portion of the absorption tower while fresh absorbent solution is fed into the upper region of the tower. The normally gaseous mixture, freed largely from the H₂ S, emerges from the upper portion of the tower, and the loaded absorbent solution, which contains the selectively absorbed H₂ S, leaves the tower near or at its bottom. Preferably, the inlet temperature of the absorbent solution during the absorption step is in the range of from about 20° to about 100° C., and more preferably from 40° to about 60° C. Pressures may vary widely; acceptable pressures are between 5 and 2000 psia, preferably 20 to 1500 psia, and most preferably 25 to 1000 psia in the absorber. The contacting takes place under conditions such that the H₂ S is selectively absorbed by the solution. The absorption conditions and apparatus are designed so as to minimize the residence time of the liquid in the absorber to reduce CO₂ pickup while at the same time maintaining sufficient residence time of gas mixture with liquid to absorb a maximum amount of the H₂ S gas. The amount of liquid required to be circulated to obtain a given degree of H₂ S removal will depend on the chemical structure and basicity of the amino compound and on the partial pessure of H₂ S in the feed gas. Gas mixtures with low partial pressures such as those encountered in thermal conversion processes will require more liquid under the same absorption conditions than gases with higher partial pressures such as shale oil retort gases.

A typical procedure for the selective H₂ S removal phase of the process comprises selectively absorbing H₂ S via countercurrent contact of the gaseous mixture containing H₂ S and CO₂ with the aqueous solution of the amino compound in a column containing a plurality of trays at a low temperature, e.g., below 45° C., and at a gas velocity of at least about 0.3 ft/sec (based on "active" or aerated tray surface), depending on the operating pressure of the gas, said tray column having fewer than 20 contacting trays, with, e.g., 4-16 trays being typically employed.

After contacting the normally gaseous mixture with the absorbent solution, which becomes saturated or partially saturated with H₂ S, the solution may be at least partially regenerated so that it may be recycled back to the absorber. As with absorption, the regeneration may take place in a single liquid phase. Regeneration or desorption of the acid gases from the absorbent solution may be accomplished by conventional means such as pressure reduction of the solution or increase of temperature to a point at which the absorbed H₂ S flashes off, or by passing the solution into a vessel of similar construction to that used in the absorption step, at the upper portion of the vessel, and passing an inert gas such as air or nitrogen or preferably steam upwardly through the vessel. The temperature of the solution during the regeneration step should be in the range from about 50° to about 170° C., and preferably from about 80° to 120° C., and the pressure of the solution on regenerator should range from about 0.5 to about 100 psia, preferably 1 to about 50 psia. The absorbent solution, after being cleansed of at least a portion of the H₂ S gas, may be recycled back to the absorbing vessel. Makeup absorbent may be added as needed.

In the preferred regeneration technique, the H₂ S-rich solution is sent to the regeneration wherein the absorbed components are stripped by the steam which is generated by reboiling the solution. Pressure in the flash drum and stripper is usually 1 to about 50 psia, preferably 15 to about 30 psia, and the temperature is typically in the range from about 50° to 170° C., preferably about 80° to 120° C. Stripper and flash temperatures will, of course, depend on stripper pressure; thus at about 15 to 30 psia stripper pressures, the temperature will be about 80° to about 120° C. during desorption. Heating of the solution to be regenerated may very suitably be effected by means of indirect heating with low-pressure steam. It is also possible, however, to use direct injection of steam.

In one embodiment for practicing the entire process herein, as illustrated in FIG. 1, the gas mixture to be purified is introduced through line 1 into the lower portion of a gas-liquid countercurrent contacting column 2, said contacting column having a lower section 3 and an upper section 4. The upper and lower sections may be segregated by one or a plurality of packed beds as desired. The absorbent solution as described above is introduced into the upper portion of the column through a pipe 5. The solution flowing to the bottom of the column encounters the gas flowing countercurrently and dissolves the H₂ S preferentially. The gas freed from most of the H₂ S exits through a pipe 6 for final use. The solution, containing mainly H₂ S and some CO₂, flows toward the bottom portion of the column, from which it is discharged through pipe 7. The solution is then pumped via optional pump 8 through an optional heat exchanger and cooler 9 disposed in pipe 7, which allows the hot solution from the regenerator 12 to exchange heat with the cooler solution from the absorber column 2 for energy conservation. The solution is entered via pipe 7 to a flash drum 10 equipped with a line (not shown) which vents to line 13 and then introduced by 11, into the upper portion of the regenerator 12, which is equipped with several plates and effects the desorption of the H₂ S and CO₂ gases carried along in the solution. This acid gas mixture is passed through a pipe 13 into a condenser 14 wherein cooling and condensation of water and amine solution from the gas occur. The gas then enters a separator 15 where further condensation is effected. The condensed solution is returned through pipe 16 to the upper portion of the regenerator 12. The gas remaining from the condensation, which contains H₂ S and some CO₂, is removed through pipe 17 for final disposal (e.g., to a vent or incinerator or an apparatus which converts the H₂ S to sulfur, such as a Claus unit or a Stretford conversion unit (not shown)).

The solution is liberated from most of the gas which it contains while flowing downward through the regenerator 12 and exits through pipe 18 at the bottom of the regenerator for transfer to a reboiler 19. Reboiler 19, equipped with an external source of heat (e.g., steam injected through pipe 20 and the condensate exits through a second pipe (not shown)), vaporizes a portion of this solution (mainly water) to drive further H₂ S therefrom. The H₂ S and steam driven off are returned via pipe 21 to the lower section of the regenerator 12 and exited through pipe 13 for entry into the condensation stages of gas treatment. The solution remaining in the reboiler 19 is drawn through pipe 22, cooled in heat exchanger 9, and introduced via the action of pump 23 (optional if pressure is sufficiently high) through pipe 5 into the absorber column 2.

The amino compounds herein are found to be superior to those used in the past, particularly to MDEA and DEAE, in terms of both selectivity and capacity for maintaining selectivity over a broad loading range. Typically, a gaseous stream to be treated having a 1:10 mole ratio of H₂ S:CO₂ from an apparatus for thermal conversion of heavy residual oil, or a Lurgi coal gas having a mole ratio of H₂ S:CO₂ of less than 1:10 will yield an acid gas having a mole ratio of H₂ S:CO₂ of about 1:1 after treatment by the process of the present invention. The process herein may be used in conjunction with another H₂ S selective removal process; however, it is preferred to carry out the process of this invention by itself, since the amino compounds are extremely effective by themselves in preferential absorption of H₂ S.

The invention is illustrated further by the following examples, which, however, are not to be taken as limiting in any respect. All parts and percentages, unless expressly stated to be otherwise, are by weight.

EXAMPLE 1 (Control) Preparation of tertiarybutylaminoethoxyethanol

736 g of tertiarybutylamine and 500 g of 2-chloroethoxyethanol were placed in 2 liters of ethanol and heated at 60° C. overnight. The temperature was then gradually raised to 80° C. and held for 5 days. The reaction mixture was cooled to 50° C. and then treated with 247 g of KOH. After 1 hour at refluxing the reaction was cooled, filtered, vacuum stripped and distilled. The yield of the distilled product, which calculates as a 75.6% yield, was 491 g, and it had a b.p. of 117° C. at 10 mm. Analysis calculated for C₈ H₁₉ NO₂ : % C 59.63; %H, 11.80, %N, 8.70; Found: % C, 58.99, %H, 11.82; %N, 8.38.

EXAMPLE 2 Preparation of tertiarybutylaminoethoxyethanol

A solution of 41.76 g of tertiarybutylamine and 28.66 g of 2-chloroethoxyethanol in 115 ml of ethanol was charged to a 300 ml metal autoclave and heated under autogenous pressure at 150° C. for 3 hr. The contents of the cooled reactor were treated with KOH and the product isolated as described in Example 1. The yield of product was 77% based on 28.65 g of recovered product. Thus, it can be seen that the high temperature has a dramatic effect on the rate of producing the severely sterically hindered amino ether alcohol.

EXAMPLE 3 Preparation of tertiarybutylaminoethoxyethanol (TBEE)

A solution of 45.63 g (0.625 mole) of tertiary-butylamine and 31 g (0.25 mole) of 2-chloroethoxyethanol in 100 ml of methanol was charged to a 300 ml steel autoclave and heated under autogenous pressure for 1 hour at 150° C. The reactor was cooled and the contents removed. To the homogeneous solution was added 11 g (0.275 mole) of NaOH pellets and the reaction refluxed for 0.5-1 hour, cooled, filtered, vacuum stripped, and distilled. The yield was 31.4 g (78%).

EXAMPLE 4 Preparation of tertiarybutylaminoethoxyethanol (TBEE)

The following example demonstrates the use of water as the polar solvent in preparing TBEE.

Tertiarybutylamine, 0.625 mole, 0.25 mole of 2-chloroethoxyethanol and 30 ml of water were heated for 1 hr. at 150° C. in a steel autoclave. The maximum pressure was about 85 psi. The reactor was cooled and the contents removed. To the homogeneous solution was added 11 g of NaOH and the reaction heated for one-half hour. The reaction was cooled, filtered, and distilled. Bp 121°-3° (15 mm). Yield 33.19 g (82.5%).

EXAMPLE 5

A solution of tertiarybutylamine, 2-chloroethoxyethanol, and solvent in the ratio detailed in the previous example were changed to a pressure reactor and heated at the temperature and times indicated in Table 1. The solvents employed are also shown in Table 1. The extent of TBEE formation was determined by gas chromotographic analysis.

                  TABLE 1                                                          ______________________________________                                         Solvent Effects on Rate of TBEE Formation                                      Solvent                                                                               BuOH    EtOH    MeOH   H.sub.2 O                                                                           Temperature/Time                            ______________________________________                                         % TBEE  4.0     6.6     5.3   19.6 100°/15 mins.                        % TBEE 38.0    41.8    44.7   76.5 125°/30 mins.                        ______________________________________                                    

As shown in Table 1, water, as the polar solvent, provides a rate enhancement in the production of TBEE. Also, the use of water reduces solvent costs to a negligible amount and eliminates the need for solvent recovery and enables one to enjoy low solvent/reactant concentrations. Thus, water, as the polar solvent, provides significant technical and economic advantages in producing hindered amines such as TBEE.

EXAMPLE 6 Preparation of 2-(2-isopropylamino)propoxyethanol

A total of 5.8 moles of isopropylamine, 134 g of 6-hydroxy-3-oxa-2-hexanone and 4 g of 10% Pd/C in 150 ml of ethanol were charged to an autoclave, pressured to 1110 psig with hydrogen and heated at 100° C. for 6 hours. The contents of the cooled autoclave were filtered and distilled. Yield, 169 g, b.p. 119° C. at 20 mm. Analysis calc. for C₈ H₁₉ NO₂ : %C, 59.63; %H, 11.80; %N, 8.70; Found: %C, 59.07, %H, 11.89; % N, 8.11.

EXAMPLE 7 Preparation of 2-(2-tertiarybutylamino)propoxyethanol

A total of 314 g of tertiarybutylamine, 110 g of 6-hydroxy-4-oxa-2-hexanone and 3 g 10% Pd/C in 200 ml of methanol were reacted under 1280 psig of hydrogen at 100° C. for 7 hr. Isolation of product as described in Example 3 yielded 20.8 g of the titled amine, which had a b.p of 122° C. at 19 mm. Analysis calcd. for C₉ H₂₁ NO₂ : %N, 8.00; Found % N, 7.28.

EXAMPLE 8 Preparation of (1-methyl-1-ethylpropylamino)ethoxyethanol

A solution of 124.7 g of 1-methyl-1-ethylpropylamine and 76.9 g of 2-chloroethoxyethanol in 300 ml of ethylene glycol monomethylether was refluxed overnight. The reaction mixture was treated with a stoichiometric excess of KOH and refluxed for one hour, filtered, and distilled. The product had a b.p. of 153° C. (2 mm). Analysis calculated for C₁₀ H₂₃ NO₂ :% N, 7.4, found %N, 7.15.

EXAMPLE 9 Preparation of tertiaryamylaminoethoxyethanol

In the manner described in Example 8, 129.7 g of tertiaryamylamine and 92.2 g of 2-chloroethoxyethanol yielded 86.5 g of tertiaryamylaminoethoxyethanol having a b.p. of 124° C. (10 mm).

EXAMPLE 10 (Control) Preparation of secondarybutylaminoethoxyethanol

In the manner described in Example 8, 131 g of secondarybutylamine and 93 g of 2-chloroethoxyethanol yielded 73 g of secondarybutylaminoethoxyethanol having a b.p. 120° C. (10 mm). Analysis calculated for C₈ H₁₉ NO₂ : %N, 8.70: Found: %N, 8.45.

EXAMPLE 11 Selective H₂ S removal from a mixture containing H₂ S and CO₂

FIG. 2 illustrates the sparged absorber unit, operated on a semi-batch mode, used to evaluate the selectivity for H₂ S removal of the amino compounds of the invention herein. A gas mixture comprised of 10% CO₂, 1% H₂ S and 89% N₂, expressed as volume percent, respectively, was passed from a gas cylinder (not shown) through line 30 to a meter 31 measuring the rate at which the gas is fed to the absorber. For all examples this rate was 3.6 liters per minute. The gas was then passed through line 32 to a gas chromatography column (not shown) continuously monitoring the composition of the inlet gas and through lines 33 and 34 to a sparged absorber unit 35, which is a cylindrical glass tube 45 cm high and 3.1 cm in diameter charged with 100 ml of the absorbent amine solution 36. The gas was passed through the solution at a solution temperature of 40° C., and 10-ml samples of the solution were periodically removed from the bottom of the absorber unit through lines 34 and 37 to be analyzed for H₂ S and CO₂ content. The H₂ S content in the liquid sample was determined by titration with silver nitrate. The CO₂ content of the liquid sample was then analyzed by acidifying the sample with an aqueous solution of 10% HCl and measuring the evolved CO₂ by weight gain on NaOH-coated asbestos.

While the solution was being periodically withdrawn from the bottom of the absorber unit, the gas mixture was removed from the top thereof via line 38 to a trap 39 which served to scrub out any H₂ S in the outlet gas. The resulting gas could optionally then be passed via lines 40 and 41 for final disposal or via line 42 to a gas chromatography column (not shown) for periodic evaluation of the composition of the outlet gas to check for system leaks. For purposes of the examples, the H₂ S and CO₂ contents of the inlet gas phase were measured and the H₂ S and CO₂ contents of the liquid phase were determined as described above. These data were used to calculate selectivity values of the amine as defined above, which were plotted as a function of the loading of the absorbent solution with H₂ S and CO₂, in units of moles acid gas per moles of the amino compound.

In this example an aqueous 3M solution of tertiarybutylaminoethoxyethanol (TBEE) (pK_(a) =10.3, summation ⁻ E_(s) =2.10) was employed as the absorbent solution. The selectivity plot of TBEE is indicated in FIG. 3.

EXAMPLE 12

The procedure of Example 11 was repeated using as the absorbent solution a 3M solution of tertiary-butylaminoethanol (TBE) (pK_(a) =10.2, b.p.=90° C. at 25 mm). The selectivity plot of TBE is indicated in FIG. 3.

EXAMPLE 13

The procedure of Example 11 was repeated using as the absorbent solution a 3M solution of methyldiethanolamine (MDEA). The selectivity plot of MDEA is also indicated in FIG. 3.

As can be seen from FIG. 3, TBEE is superior to both TBE and especially MDEA in terms of H₂ S selectivity, particularly at high H₂ S and CO₂ loadings. It is noteworthy that TBEE is superior to TBE even though both compounds have a pK_(a) of about 10.3.

EXAMPLE 14

The procedure of Example 11 was repeated using as the absorbent solution a 3M solution of tertiarybutylaminoethoxyethanol (TBEE) (summation ^(-E) _(s) of 2.10), secondarybutylaminoethoxyethanol (SBEE) (Taft ^(-E) _(s) of 1.32 as prepared in Example 7 (Control), isopropylaminoethoxyethanol (IPEE) (summation ^(-E) _(s) of 1.29) and methyldiethanolamine (MDEA) (summation ^(-E) _(s) of 0.79). The selectivity plot for each amine solution is shown in FIG. 4. The plots clearly show that TBEE is far superior to SBEE, IPEE and MDEA in terms of H₂ S selectivity. The plots taken together with the summation of Taft ^(-E) _(s) values for the compounds tested also indicate that the severe steric hindrance of TBEE (resulting from the additional carbon atoms attached to the carbon atom directly attached to the nitrogen atom) has a profound effect on the selective H₂ S absorption properties of the compound.

The data in FIG. 3 also show that the amino compounds of the present invention have very high capacity for both H₂ S and CO₂ compared to methyldiethanolamine (MDEA) in addition to high H₂ S selectivities. It will be apparent from an inspection of the data in FIG. 3 that if the absorption process is conducted under conditions such that the amino compound has a long contact time with the gases to be absorbed, the selectivity for H₂ S decreases, but the overall capacity for both CO₂ and H₂ S remains rather high. Therefore, one may, in some instances, wish to carry out a "non-selective" absorption process to take advantage of the large absorption capacity of the amino compounds of the invention. Accordingly, one may carry out a "non-selective" acid gas removal absorption process using the amino compounds of the invention. Such "non-selective" processes are particularly useful in scrubbing natural gases which contain relatively high levels of H₂ S and low to nil levels of CO₂. As such, the amino compounds of the invention may replace some or all of the monoethanolamine (MEA) or diethanolamine (DEA) commonly used for such scrubbing processes.

These amino compounds are capable of reducing the H₂ S in gaseous mixtures to a relatively low level, e.g., less than about 200 Vppm and have a relatively high capacity for H₂ S, e.g., greater than about 0.5 mole of H₂ S per mole of amine. The amino compounds are characterized as having a "kinetic selectivity" for H₂ S, i.e., a faster reaction rate for H₂ S than for CO₂ at absorption conditions. In addition they have a higher capacity for H₂ S at equivalent kinetic selectivity for H₂ S over CO₂. This higher capacity results in the economic advantage of lower steam requirements during regeneration.

EXAMPLE 15 Continuous Process for Selective H₂ S Removal

This example demonstrates a comparison of the severely sterically hindered secondary aminoether alcohol, tertiarybutylaminoethoxyethanol (TBEE), with methyldiethanolamine (MDEA) using a unit such as that shown in FIG. 1.

A 1.5M aqueous solution of tertiarybutylaminoethoxyethanol (TBEE) was charged via pipe 5 into the upper portion of a gas-liquid countercurrent absorption column 2 having a lower Section 3 and an upper Section 4 and being segregated by three packed beds. The gas to be purified was a synthetic mixture containing 1% H₂ S, 11% CO₂ and 88% N₂, expressed in volume percent, respectively. The gas was introduced through line 1 into the lower portion of column 2 at a gas flow rate of 67 standard cubic feet per minute. The absorber pressure was adjusted to 31 psia. The gas freed from H₂ S exited through pipe 6 and was analyzed. The aqueous amine solution containing H₂ S and CO₂ was flowed toward the lower portion of the absorber, from which it was discharged through pipe 7. The solution was then passed via pump 8 through a simulated heat exchanger and cooler 9 disposed in pipe 7, which allowed the hot solution from the regenerator 12 to equilibrate in temperature with the cooler solution from the absorber column 2. The hot rich solution was then entered via pipe 7 to a flash drum 10 equipped with a line (not shown) which vents to line 13 and then introduced by pipe 11 in to the upper portion of the regenerator 12 to effect desorption of the H₂ S gas. The pressure of the regenerator was set at 33 psia. The H₂ S gas was passed through a pipe 13 into a condenser 14 wherein cooling and condensation of water and amine solution from the gas occurred. The gas was then entered into a separator 15 where further condensation took place. The condensed solution was returned through pipe 16 to the upper portion of the regenerator 12. The gas remaining from the condensation which contains H₂ S and some CO₂ may be removed through pipe 17 for final disposal (e.g., to a vent or incinerator or to an apparatus which converts the H₂ S to sulfur such as a Claus unit or a Stretford conversion unit (not shown)). The solution liberated from the gas which it contained was flowed downward through the regenerator 12 and exited through pipe 18 at the bottom of the regenerator for transfer to a reboiler 19. Reboiler 19, equipped with a steam injection pipe 20 and a condensate exit pipe (not shown), vaporized a portion of this solution to drive additional H₂ S therefrom. The H₂ S driven off was returned via pipe 21 to the lower section of the regenerator 12 and exited through pipe 13 for entry into the condensation stages of gas treatment. The solution remaining in the reboiler 19 was drawn through pipe 22, cooled in heat exchanger 9, and introduced via the action of pump 23 through pipe 5 into absorber 2.

The flow rate was slowly adjusted downward until the H₂ S leak rate showed a dramatic increase.

The experiment was repeated using in place of tertiarybutylaminoethoxyethanol (TBEE), a 3M aqueous solution of methyldiethanolamine (MDEA). The results of both experiments were plotted wherein the H₂ S leak rate, in parts per million by volume (Vppm), was plotted against H₂ S loading in mols/mol amine. The results are shown in FIG. 5. These results show that tertiarybutylaminoethoxyethanol gives far greater cleanup, even at higher H₂ S loadings, in a continuous selective H₂ S removal process than methyldiethanolamine (MDEA).

In summary, this invention is seen to provide a special class of amino compounds characterized as being severely hindered acyclic secondary aminoether alcohols having a high selectivity for H₂ S in preference to CO₂ which selectivity is maintained at high H₂ S and CO₂ loading levels.

While the invention has been described in connection with specific embodiments thereof, it will be understood that it is capable of further modification, and this application is intended to cover any variations, uses, or adaptations of the invention following, in general, the principles of the invention and including such departures from the present disclosure as come within known or customary practice in the art to which the invention pertains and as may be applied to the essential features hereinbefore set forth, and as fall within the scope of the invention. 

What is claimed is:
 1. A process for preparing a secondary aminoether alcohol comprising reacting, at elevated temperatures, a secondary or tertiary alkyl primary amine with a haloalkoxyalkanol in the presence of a solvent.
 2. The process of claim 1 wherein the tertiary alkyl primary amine is tertiary butylamine, the haloalkoxyalkanol is 2-chloroethoxyethanol, and the solvent is selected from water, methanol, ethanol and ethylene glycol monomethylether which reaction is conducted at the temperature of at least 110° C. at autogenous pressure to produce tertiarybutylaminoethoxyethanol.
 3. A process for preparing a secondary aminoether alcohol comprising reacting, at elevated temperatures, a secondary or tertiary alkyl primary amine with an ether alcohol containing a carbonyl functionality in the presence of a source of hydrogen.
 4. The process of claim 2 wherein the process is carried out at temperatures ranging from 125° C. to about 200° C. 